CN116078118A - Organic waste gas treatment system and method - Google Patents
Organic waste gas treatment system and method Download PDFInfo
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- CN116078118A CN116078118A CN202310369417.4A CN202310369417A CN116078118A CN 116078118 A CN116078118 A CN 116078118A CN 202310369417 A CN202310369417 A CN 202310369417A CN 116078118 A CN116078118 A CN 116078118A
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- 239000007789 gas Substances 0.000 title claims abstract description 104
- 239000010815 organic waste Substances 0.000 title claims abstract description 81
- 238000011282 treatment Methods 0.000 title claims abstract description 47
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000010521 absorption reaction Methods 0.000 claims abstract description 170
- 239000007788 liquid Substances 0.000 claims abstract description 167
- 238000011084 recovery Methods 0.000 claims abstract description 43
- 239000003960 organic solvent Substances 0.000 claims abstract description 38
- 238000000926 separation method Methods 0.000 claims abstract description 36
- 238000005507 spraying Methods 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 26
- 238000001816 cooling Methods 0.000 claims description 22
- 239000002904 solvent Substances 0.000 claims description 20
- 238000005406 washing Methods 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 14
- 239000007921 spray Substances 0.000 claims description 12
- 239000000428 dust Substances 0.000 claims description 5
- 239000012075 bio-oil Substances 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 239000002912 waste gas Substances 0.000 abstract description 12
- 238000004064 recycling Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 2
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 12
- 238000003795 desorption Methods 0.000 description 11
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 10
- 238000010586 diagram Methods 0.000 description 8
- 238000009835 boiling Methods 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 125000004123 n-propyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])* 0.000 description 4
- 238000007639 printing Methods 0.000 description 4
- DCKVNWZUADLDEH-UHFFFAOYSA-N sec-butyl acetate Chemical compound CCC(C)OC(C)=O DCKVNWZUADLDEH-UHFFFAOYSA-N 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- LRHPLDYGYMQRHN-UHFFFAOYSA-N butyl alcohol Substances CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 1
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000011221 initial treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
- B01D53/145—Pretreatment by separation of solid or liquid material
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
- B01D2252/2021—Methanol
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/704—Solvents not covered by groups B01D2257/702 - B01D2257/7027
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses an organic waste gas treatment system and method, and relates to the field of waste gas treatment. The organic waste gas treatment system comprises the following subsystems which are connected in sequence: the precooling subsystem is used for precooling the organic waste gas; an absorption subsystem for absorbing the organic solvent in the organic waste gas by the absorption liquid; the separation subsystem is used for desorbing the absorption liquid and circulating the desorbed absorption liquid to the absorption subsystem; the absorption subsystem comprises an absorption tower and a recovery tower which are connected in sequence. The invention adopts the biological oil multistage absorption and biological oil recycling process, which can greatly improve the removal rate of the organic solvent in the waste gas, effectively reduce the energy consumption and greatly reduce the operation cost.
Description
Technical Field
The invention relates to the field of waste gas treatment, in particular to an organic waste gas treatment system and method.
Background
In the production process of the gravure industry, a large amount of medium-high concentration organic waste gas is generated, and the concentration of the organic waste gas is generally 800-3000 mg/m 3 These organic off-gases mainly include ethyl acetate, n-propyl, butyl and isopropyl alcohol. For organic waste gas, the existing treatment modes mainly comprise: activated carbon adsorption, RTO treatment, and CTO treatment. The activated carbon adsorption method can only be applied to treating low-concentration organic waste gas, and the concentration of the organic waste gas is hardly reduced obviously when the on-site detection is carried out due to the fact that the adsorption amount of the activated carbon is too low for medium-high-concentration organic waste gas. For a pair ofIn the RTO or CTO treatment method, since the organic waste gas needs to be burned, a large amount of fossil energy is consumed, and the operation cost is high; if the organic waste gas is generated in an unstable way for enterprises in the intaglio printing industry, the operation cost is higher, and because the concentration of the organic waste gas is too low, the heat generated by combustion is insufficient, and more fossil fuel is required to be used for ensuring the sufficient combustion, the operation cost is higher. The concentration of the organic waste gas is 800-3000 mg/m 3 To calculate, process 30000m 3 The cost of the natural gas per day of the organic waste gas per hour is up to 1-2 ten thousand according to the existing price of the natural gas, and the burden of enterprises is greatly increased.
It can be seen that there is a need for improvements and improvements in the art.
Disclosure of Invention
In view of the above-mentioned shortcomings of the prior art, the present invention aims to provide an organic waste gas treatment system and method, which aims to solve the technical problem of high treatment cost of medium-high concentration organic waste gas generated in the printing industry in the prior art.
In order to achieve the above purpose, the invention adopts the following technical scheme:
an organic waste gas treatment system comprising the following subsystems connected in sequence: the precooling subsystem is used for precooling the organic waste gas; an absorption subsystem for absorbing the organic solvent in the organic waste gas by the absorption liquid; the separation subsystem is used for desorbing the absorption liquid and circulating the desorbed absorption liquid to the absorption subsystem; the absorption subsystem comprises an absorption tower and a recovery tower which are connected in sequence; the bottom of the absorption tower is provided with: the first connecting port is used for being connected with the air outlet end of the precooling subsystem; the second connecting port is used for being connected with the liquid outlet end of the recovery tower; the third connecting port is used for being connected with the liquid inlet end of the separation subsystem; a first spray device is arranged in the absorption tower, and the liquid inlet end of the first spray device is communicated with the bottom or the liquid outlet end of the absorption tower; the top of the absorption tower is provided with a first exhaust port, and the first exhaust port is connected with the air inlet end of the recovery tower; a second spraying device is arranged in the recovery tower, and the liquid inlet end of the second spraying device is connected with the absorption liquid outlet of the separation subsystem; the top of the absorption tower is provided with a second exhaust port.
The organic waste gas treatment system further comprises a liquid collecting box, wherein the liquid inlet end of the liquid collecting box is connected with the liquid outlet end of the absorption tower, and the liquid outlet end of the liquid collecting box is connected with the liquid inlet end of the separation subsystem.
The organic waste gas treatment system comprises a precooling subsystem and a first cooling device, wherein the precooling subsystem comprises a filter and a first cooling device which are connected in sequence, and the filter is used for removing dust particles in organic waste gas; the first cooler is used for reducing the temperature of organic waste gas, and the air outlet end of the first cooler is connected with the first connecting port.
The organic waste gas treatment system comprises a separation subsystem and a separation subsystem, wherein the separation subsystem comprises a heating device and an evaporator which are sequentially connected; the downstream of the evaporator is also provided with a solvent recovery device and an absorption liquid storage tank; the solvent recovery device is connected with the top of the evaporator; the liquid inlet end of the absorption liquid storage tank is connected with the bottom of the evaporator, and the liquid outlet end of the absorption liquid storage tank is connected with the liquid inlet end of the second spraying device.
And the organic waste gas treatment system comprises a solvent recovery device, wherein the solvent recovery device comprises a second cooler and a solvent tank which are sequentially connected.
The organic waste gas treatment system comprises a first cooler and a second cooler, wherein the first cooler comprises a water chiller and a first heat exchanger, a first heat exchange pipeline and a second heat exchange pipeline are arranged in the first heat exchanger, and two ends of the first heat exchange pipeline are respectively connected with the evaporator and the solvent tank; and two ends of the second heat exchange pipeline are respectively connected with a water inlet end and a water outlet end of the water chiller.
The organic waste gas treatment system further comprises a second heat exchanger, a third heat exchange pipeline and a fourth heat exchange pipeline are arranged in the second heat exchanger, and two ends of the third heat exchange pipeline are respectively connected with the third connection port and the liquid inlet end of the heating device; and two ends of the fourth heat exchange pipeline are respectively connected with the bottom of the evaporator and the absorption liquid storage tank.
The organic waste gas treatment system further comprises a washing tower, and the air inlet end of the washing tower is connected with the air outlet end of the top of the recovery tower.
And the organic waste gas treatment system is characterized in that a third spraying device is arranged in the washing tower, and the liquid inlet end of the third spraying device is connected with the bottom of the washing tower.
An organic waste gas treatment method adopts the organic waste gas treatment system to treat organic waste gas, and the absorption liquid is bio-oil.
Advantageous effects
The first aspect of the invention provides an organic waste gas treatment system, which comprises a precooling subsystem, an absorption subsystem and a separation subsystem, wherein the absorption subsystem comprises an absorption tower and a recovery tower, a multistage absorption process is adopted, absorption liquid firstly passes through the recovery tower and then enters the absorption tower, organic waste gas firstly enters the absorption tower and then enters the recovery tower, the first-stage process is to treat high-concentration organic waste gas by adopting the absorption liquid containing organic solvent, the second-stage process is to treat low-concentration organic waste gas by adopting the recovered absorption liquid, the removal rate of the medium-high-concentration organic waste gas is greatly improved, the system can achieve the removal rate of more than 97%, the absorption liquid can be recycled and the organic solvent can be recovered by the separation subsystem, and the operation cost is greatly reduced. In addition, the organic waste gas treatment system of the invention has wide application range, and the concentration of the organic waste gas is 300-3500 mg/m 3 The method is applicable to the time and covers organic waste gas with low, medium and high concentration.
The second aspect of the invention provides an organic waste gas treatment method, which adopts the organic waste gas treatment system provided by the invention and biological oil as absorption liquid, can efficiently absorb ethyl acetate, n-propyl ester, butyl ester and isopropanol in waste gas, and can efficiently carry out desorption in a separation subsystem, and has high operation efficiency.
Drawings
Fig. 1 is a schematic diagram of an organic exhaust gas treatment system.
Fig. 2 is a schematic diagram of a pre-cooling subsystem.
Fig. 3 is a schematic diagram of an absorption subsystem in one embodiment.
FIG. 4 is a schematic diagram of a separation subsystem in one embodiment.
FIG. 5 is a schematic diagram of a separation subsystem according to an embodiment.
FIG. 6 is a schematic diagram of a separation subsystem in one embodiment.
FIG. 7 is a schematic diagram of a separation subsystem in one embodiment.
Fig. 8 is a schematic diagram of a second embodiment of an organic exhaust gas treatment system.
Description of main reference numerals: 100-precooling subsystem, 101-filter, 102-first cooler, 103-cooling tower, 200-absorption subsystem, 201-absorption tower, 202-recovery tower, 203-first spray device, 204-second spray device, 205-washing tower, 206-third spray device, 207-induced draft fan, 208-washing liquid pump, 209-header tank, 210-first absorption liquid pump, 211-second absorption liquid pump, 300-separation subsystem, 301-heating device, 302-evaporator, 303-solvent recovery device, 304-absorption liquid storage tank, 305-third absorption liquid pump, 306-fourth absorption liquid pump, 307-second cooler, 3071-chiller, 3072-first heat exchanger, 308-solvent tank, 309-second heat exchanger, 310-third heat exchanger, 311-evacuation pump, 312-fourth heat exchanger.
Detailed Description
The invention provides an organic waste gas treatment system and method, which are used for making the purposes, technical schemes and effects of the invention clearer and more definite, and the invention is further described in detail below by referring to the attached drawings and examples. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
In the description of the present invention, it should be understood that the terms "upper," "lower," "left," "right," and the like indicate an orientation or a positional relationship based on that shown in the drawings, and are merely for convenience of description and for simplifying the description, and do not indicate or imply that the apparatus or element in question must have a specific orientation, as well as a specific orientation configuration and operation, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature.
Referring to fig. 1 and 8, a first aspect of the present invention provides an organic exhaust gas treatment system, comprising the following subsystems connected in sequence:
a pre-cooling subsystem 100 for pre-cooling the organic waste gas; in the printing industry, organic waste gas mainly comprises organic solvents such as ethyl acetate, n-propyl ester, butyl ester, isopropanol and the like, the temperature of the organic waste gas is generally 40-60 ℃, and the stability of organic matters is poor at the temperature and is not beneficial to absorption of absorption liquid;
an absorption subsystem 200 for absorbing the organic solvent in the organic waste gas by the absorption liquid;
the separation subsystem 300 is used for desorbing the absorption liquid and circulating the desorbed absorption liquid to the absorption subsystem 200;
the absorption subsystem 200 comprises an absorption tower 201 and a recovery tower 202 which are connected in sequence;
the bottom of the absorption tower 201 is provided with: a first connection port, configured to connect with an air outlet end of the precooling subsystem 100; the second connection port is used for being connected with the liquid outlet end of the recovery tower 202; the third connection port is used for being connected with the liquid inlet end of the separation subsystem 300; a first spraying device 203 is arranged in the absorption tower 201, and a liquid inlet end of the first spraying device 203 is communicated with a bottom or a liquid outlet end of the absorption tower 201; a first exhaust port is arranged at the top of the absorption tower 201 and is connected with the air inlet end of the recovery tower 202; specifically, the first connection port is located below the first spraying device 203.
A second spraying device 204 is arranged in the recovery tower 202, and a liquid inlet end of the second spraying device 204 is connected with an absorption liquid outlet of the separation subsystem 300; a second exhaust port is provided at the top of the absorption tower 201. The inlet of the recovery tower 202 is located below the second spraying device 204.
In operation, after desorption and recovery of the absorption liquid in the separation subsystem 300, the absorption liquid is conveyed into the second spraying device 204 of the recovery tower 202 and then contacts with the organic waste gas which is subjected to primary treatment, and a small amount of residual organic solvent in the absorption liquid is absorbed; then, the absorbing liquid at the bottom of the recovery tower 202 is conveyed to the bottom of the absorption tower 201, at this time, the absorbing liquid at the bottom of the absorption tower 201 is mixed with the absorbing liquid sprayed from the upper part to form the absorbing liquid containing the high-concentration organic solvent, and the first spraying device 203 is used for spraying by recycling the absorbing liquid at the bottom of the absorption tower 201, so that the high-concentration organic waste gas is changed into the low-concentration organic waste gas, and the low-concentration organic waste gas enters the recovery tower 202 for the secondary absorption process. A part of the absorption liquid at the bottom of the absorption tower 201 is delivered to the first spraying device 203 for spraying, and the other part is delivered to the separation subsystem 300 for desorption, so that the recycling of the absorption liquid is completed.
Specifically, the first spraying device 203 is connected to the bottom or the liquid outlet end of the absorption tower 201 through an absorption liquid circulation pipeline, and a first absorption liquid pump 210 is disposed on the absorption liquid circulation pipeline, where the first absorption liquid pump 210 is used for providing power to circulate and spray a part of the absorption liquid at the bottom of the absorption tower 201.
Specifically, a plurality of layers of grid plates are further disposed in the absorption tower 201, and spray openings of the first spraying device 203 are respectively disposed above each layer of grid plates. The grid plates are used for enabling the organic waste gas to uniformly pass through the absorption tower 201, enabling the absorption liquid to be in contact with the organic waste gas more uniformly, and enabling the removal effect of the organic solvent to be better.
A plurality of packing layers are arranged in the recovery tower 202, and spray ports of a second spray device 204 are respectively arranged above each layer of grid plates. The packing layer also serves to uniformly pass the exhaust gas through the recovery tower 202. The top of the recovery tower 202 is provided with a water removal layer for removing moisture from the gas.
Referring to fig. 3, in one embodiment, the absorption subsystem 200 further includes a header tank 209, a liquid inlet end of the header tank 209 is connected to a liquid outlet end of the absorption tower 201, and a liquid outlet end of the header tank 209 is connected to a liquid inlet end of the separation subsystem 300. The header tank 209 temporarily stores the absorption liquid discharged from the absorption tower 201.
Specifically, a second absorption liquid pump 211 is disposed between the header tank 209 and the separation subsystem 300, and the second absorption liquid pump 211 is used for sending the absorption liquid discharged from the absorption subsystem 200 into the separation subsystem 300.
Referring to fig. 2, in one embodiment, the pre-cooling subsystem 100 includes a filter 101 and a first cooler 102 connected in sequence, where the filter 101 is used to remove dust particles in the organic exhaust gas; the first cooler 102 is configured to reduce the temperature of the organic waste gas, and the air outlet end of the first cooler 102 is connected with the first connection port.
Referring to fig. 2, in one embodiment, the first cooler 102 is a plate heat exchanger, a cooling pipe and a gas pipe are disposed in the plate heat exchanger, two ends of the cooling pipe are connected to the cooling tower 103, the gas pipe is used for passing through organic waste gas, a medium in the cooling pipe is cold water, and in this embodiment, the circulating cold water generated by the cooling tower 103 cools the waste gas.
Referring to fig. 4 and 8, in one embodiment, the separation subsystem 300 includes a heating device 301 and an evaporator 302 connected in sequence; a solvent recovery device 303 and an absorption liquid storage tank 304 are also arranged at the downstream of the evaporator 302; the solvent recovery device 303 is connected with the top of the evaporator 302; the liquid inlet end of the absorption liquid storage tank 304 is connected to the bottom of the evaporator 302, and the liquid outlet end thereof is connected to the liquid inlet end of the second spraying device 204. The heating device 301 is used for heating the absorption liquid to achieve desorption of the absorption liquid by the difference in boiling point between the organic solvent and the absorption liquid. In the printing industry, the boiling point of the organic solvent of the waste gas is lower, for example, the boiling point of ethyl acetate is 76.6-77.5 ℃, the boiling point of n-propyl ester is 102 ℃, the boiling point of butyl ester is 125-126 ℃ and the boiling point of isopropyl alcohol is 82.45 ℃, the boiling point of the absorption liquid is above 300 ℃, and when the absorption liquid is heated to above 160 ℃, the organic solvent can be fully desorbed from the absorption liquid. The desorbed organic solvent gas is discharged from the top of the evaporator 302 and the desorbed absorption liquid enters the absorption liquid storage tank 304. Preferably, the heating device 301 uses a steam heating heat exchanger to transfer heat to the absorption liquid in the conveying pipeline through a steam pipeline, specifically, the temperature of the steam is about 175 ℃, the temperature of the heated absorption liquid can reach 160 ℃ rapidly, and after the high-temperature absorption liquid reaches the evaporator 302 with larger volume, the organic solvent in the absorption liquid is desorbed from the absorption liquid.
Referring to fig. 5, specifically, the evaporator 302 is connected to the absorption liquid storage tank 304 through a pipeline, and a third absorption liquid pump 305 is disposed on the pipeline, and the third absorption liquid pump 305 is used for providing conveying power.
Referring to fig. 5, the absorption liquid storage tank 304 is connected to the second spraying device 204 through a pipeline, and a fourth absorption liquid pump 306 is disposed on the pipeline, and the fourth absorption liquid pump 306 is used for conveying the desorption absorption liquid in the absorption liquid storage tank 304 to the recovery tower 202 for recycling.
Referring to fig. 5, in one embodiment, the solvent recovery device 303 includes a second cooler 307 and a solvent tank 308 sequentially connected. The second temperature reducer 307 is used for reducing the temperature of the organic solvent gas to liquefy the organic solvent gas. The solvent tank 308 is used to collect the liquefied organic solvent.
Referring to fig. 5, in one embodiment, the second cooling device 307 includes a chiller 3071 and a first heat exchanger 3072, a first heat exchange pipeline and a second heat exchange pipeline are disposed in the first heat exchanger 3072, and two ends of the first heat exchange pipeline are respectively connected with the evaporator 302 and the solvent tank 308; two ends of the second heat exchange pipeline are respectively connected with a water inlet end and a water outlet end of the water chiller 3071. The water chiller 3071 is used for preparing cold water, and the cold water is conveyed to the second heat exchange pipeline to exchange heat with hot organic solvent gas in the first heat exchange pipeline, so that the organic solvent gas is cooled and liquefied. The cold water after heat exchange flows back to the water chiller 3071 for recycling.
Referring to fig. 6, in one embodiment, the separation subsystem 300 further includes a second heat exchanger 309, a third heat exchange pipeline and a fourth heat exchange pipeline are disposed in the second heat exchanger 309, and two ends of the third heat exchange pipeline are respectively connected to the third connection port and the liquid inlet end of the heating device 301; the two ends of the fourth heat exchange pipeline are respectively connected with the bottom of the evaporator 302 and the absorption liquid storage tank 304. In this embodiment, the absorption liquid first passes through the fourth heat exchange pipeline and then is conveyed into the absorption liquid storage tank 304, the temperature of the absorption liquid discharged from the absorption tower 201 in the third heat exchange pipeline is about 30 ℃, when the third heat exchange pipeline exchanges heat with the fourth heat exchange pipeline, the absorption liquid (160 ℃) after the desorption transfers heat to the absorption liquid at normal temperature, after the heat exchange, the temperature of the absorption liquid flowing into the separation system 300 is increased from 30 ℃ to 140 ℃, and the temperature of the desorption absorption liquid flowing out is reduced from 160 ℃ to 40 ℃, so that the waste heat can be effectively utilized through the second heat exchanger 309, and the heat required by the subsequent heating and desorption of the absorption liquid flowing in is reduced.
In one embodiment, the liquid outlet end of the absorption liquid storage tank 304 is further connected to the liquid inlet end of the third heat exchange pipeline through a pipeline, and a valve and a delivery pump are disposed on the pipeline. In the present embodiment, the absorption liquid in the absorption liquid storage tank 304 can be circulated through the second heat exchanger 309, the heating device 301, and the evaporator 302, and desorption can be performed a plurality of times, so that the purity of the absorption liquid can be improved.
Referring to fig. 7, in an embodiment, a third heat exchanger 310 is further disposed between the evaporator 302 and the second cooler 307, a fifth heat exchange pipeline and a sixth heat exchange pipeline are disposed in the third heat exchanger 310, and two ends of the fifth heat exchange pipeline are respectively connected with the top of the evaporator 302 and the liquid inlet end of the first heat exchange pipeline; both ends of the sixth heat exchange pipe are connected to the cooling tower 103. Cold water flows through the sixth heat exchange pipeline, the high-temperature organic solvent gas (about 160 ℃) discharged from the evaporator 302 is cooled to 40 ℃ by the cold water, and then the temperature of the organic solvent is further reduced by the second cooler 307, so that the temperature of the organic solvent reaches 15 ℃, and the desorbed organic solvent is in the most stable state at the temperature. The cooling tower 103 is used to cool the water in the pipes. The energy consumption can be reduced by cooling with cold water at normal temperature formed by the cooling tower 103 and then cooling with low-temperature cold water formed by the chiller 3071.
Referring to fig. 6, in one embodiment, a vacuum pump 311 is further disposed between the second temperature reducer 307 and the solvent tank 308, and the vacuum pump 311 can promote desorption of the organic solvent in the evaporator 302 from the absorption liquid.
Referring to fig. 7, in an embodiment, a fourth heat exchanger 312 is further disposed between the second heat exchanger 309 and the absorption liquid storage tank 304, a seventh heat exchange pipeline and an eighth heat exchange pipeline are disposed in the fourth heat exchanger 312, and two ends of the seventh heat exchange pipeline are respectively connected with the liquid outlet end of the fourth heat exchange pipeline and the liquid inlet end of the absorption liquid storage tank 304; both ends of the eighth heat exchange pipeline are respectively connected with the cooling tower 103. And cold water flows through the eighth heat exchange pipeline, and the cooled absorption liquid is further cooled by the cold water. The temperature of the desorption absorption liquid discharged from the evaporator 302 reaches 160 ℃, the temperature can be reduced to 40 ℃ after passing through the second heat exchanger 309, and then the temperature can be reduced to 30 ℃ after passing through the fourth heat exchanger 312, so that the absorption liquid near the normal temperature has better organic solvent absorption effect when being recycled to the absorption subsystem 200.
Referring to fig. 3 and 8, in one embodiment, the absorption subsystem 200 further includes a scrubber 205, and an air inlet end of the scrubber 205 is connected to an air outlet end of the top of the recovery tower 202. The scrubber 205 is used to remove very small amounts of organic solvent from the off-gas that is not sufficiently absorbed. Specifically, an induced draft fan 207 is disposed downstream of the scrubber 205, and the induced draft fan 207 is configured to facilitate the entry of the exhaust gas from the precooling subsystem 100 and the exit of the exhaust gas after passing through the absorption subsystem 200.
Referring to fig. 3 and 8, in one embodiment, a third spraying device 206 is disposed in the washing tower 205, and a liquid inlet end of the third spraying device 206 is connected to the bottom of the washing tower 205. Specifically, the liquid inlet end of the third spraying device 206 is connected to the bottom of the washing tower 205 through a washing liquid pipe, and a washing liquid pump 208 is disposed on the washing liquid pipe, so that the washing liquid circulates and sprays in the washing tower 205.
In a second aspect, the present invention provides a method for treating organic waste gas, which adopts the organic waste gas treatment system to treat organic waste gas, wherein the absorption liquid is bio-oil.
The organic waste gas treatment method comprises the following steps:
s1, removing dust in the waste gas through a separation subsystem, and reducing the temperature of the waste gas to 30 ℃;
s2, conveying the waste gas after dust removal to an absorption subsystem, sequentially passing through an absorption tower and a recovery tower, and absorbing organic solvents in the organic waste gas by the recovery tower and the absorption tower through spraying absorption liquid to obtain purified gas and absorption liquid for absorbing the organic solvents; discharging the purified gas, wherein one part of absorption liquid for absorbing the organic solvent is recycled in the absorption tower, and the other part of absorption liquid is conveyed to the separation subsystem;
s3, heating the absorption liquid entering the separation subsystem to 160 ℃ through heat exchange, and desorbing to obtain desorbed absorption liquid and organic solvent gas; cooling the desorbed absorption liquid, and conveying the cooled absorption liquid into a recovery tower for recycling; and cooling the organic solvent gas, liquefying, and collecting and storing.
In summary, the invention provides an organic waste gas treatment system and method, by which the treatment cost of organic waste gas can be greatly saved, and the system and method can be effectively applied to medium-high concentration organic solvent waste gas. The organic solvent in the waste gas does not need to burn, so that the use of fossil fuel can be greatly saved, the energy is saved, the environment is protected, and the operation cost is low. In addition, the invention can collect the organic solvent without burning the organic solvent, thereby reducing the emission of carbon dioxide. In the gravure industry, the recovered organic solvent is low in types, high in purity and easy to recycle, and can be sold at a high price of 8 kilo/ton according to the existing price, which is equivalent to further reducing the treatment cost of waste gas.
It will be understood that equivalents and modifications will occur to those skilled in the art in light of the present invention and their spirit, and all such modifications and substitutions are intended to be included within the scope of the present invention as defined in the following claims.
Claims (10)
1. An organic waste gas treatment system, comprising the following subsystems connected in sequence:
the precooling subsystem is used for precooling the organic waste gas;
an absorption subsystem for absorbing the organic solvent in the organic waste gas by the absorption liquid;
the separation subsystem is used for desorbing the absorption liquid and circulating the desorbed absorption liquid to the absorption subsystem;
the absorption subsystem comprises an absorption tower and a recovery tower which are connected in sequence;
the bottom of the absorption tower is provided with: the first connecting port is used for being connected with the air outlet end of the precooling subsystem; the second connecting port is used for being connected with the liquid outlet end of the recovery tower; the third connecting port is used for being connected with the liquid inlet end of the separation subsystem; a first spray device is arranged in the absorption tower, and the liquid inlet end of the first spray device is communicated with the bottom or the liquid outlet end of the absorption tower; the top of the absorption tower is provided with a first exhaust port, and the first exhaust port is connected with the air inlet end of the recovery tower;
a second spraying device is arranged in the recovery tower, and the liquid inlet end of the second spraying device is connected with the absorption liquid outlet of the separation subsystem; the top of the absorption tower is provided with a second exhaust port.
2. The organic waste gas treatment system of claim 1, wherein the absorption subsystem further comprises a liquid collection tank, a liquid inlet end of the liquid collection tank is connected with a liquid outlet end of the absorption tower, and a liquid outlet end of the liquid collection tank is connected with a liquid inlet end of the separation subsystem.
3. The organic waste gas treatment system of claim 1, wherein the pre-cooling subsystem comprises a filter and a first desuperheater connected in sequence, the filter being configured to remove dust particles in the organic waste gas; the first cooler is used for reducing the temperature of organic waste gas, and the air outlet end of the first cooler is connected with the first connecting port.
4. The organic exhaust gas treatment system of claim 1, wherein the separation subsystem comprises a heating device and an evaporator connected in sequence; the downstream of the evaporator is also provided with a solvent recovery device and an absorption liquid storage tank; the solvent recovery device is connected with the top of the evaporator; the liquid inlet end of the absorption liquid storage tank is connected with the bottom of the evaporator, and the liquid outlet end of the absorption liquid storage tank is connected with the liquid inlet end of the second spraying device.
5. The organic waste gas treatment system of claim 4, wherein the solvent recovery device comprises a second desuperheater and a solvent tank connected in sequence.
6. The organic waste gas treatment system according to claim 5, wherein the second cooler comprises a water chiller and a first heat exchanger, a first heat exchange pipeline and a second heat exchange pipeline are arranged in the first heat exchanger, and two ends of the first heat exchange pipeline are respectively connected with the evaporator and the solvent tank; and two ends of the second heat exchange pipeline are respectively connected with a water inlet end and a water outlet end of the water chiller.
7. The organic waste gas treatment system according to claim 4, wherein the separation subsystem further comprises a second heat exchanger, a third heat exchange pipeline and a fourth heat exchange pipeline are arranged in the second heat exchanger, and two ends of the third heat exchange pipeline are respectively connected with the third connection port and the liquid inlet end of the heating device; and two ends of the fourth heat exchange pipeline are respectively connected with the bottom of the evaporator and the absorption liquid storage tank.
8. The organic waste gas treatment system of claim 1, wherein the absorption subsystem further comprises a scrubber, an inlet end of the scrubber being connected to an outlet end of the top of the recovery tower.
9. The organic waste gas treatment system according to claim 8, wherein a third spraying device is arranged in the washing tower, and a liquid inlet end of the third spraying device is connected with the bottom of the washing tower.
10. A method for treating organic waste gas, characterized in that the organic waste gas is treated by the organic waste gas treatment system according to any one of claims 1 to 9, and the absorption liquid is bio-oil.
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| CN202310369417.4A CN116078118A (en) | 2023-04-10 | 2023-04-10 | Organic waste gas treatment system and method |
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| CN202310369417.4A CN116078118A (en) | 2023-04-10 | 2023-04-10 | Organic waste gas treatment system and method |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102179137A (en) * | 2011-05-05 | 2011-09-14 | 艾特克控股集团有限公司 | Method for treating organic waste gas |
| CN104801156A (en) * | 2015-04-09 | 2015-07-29 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Method for recovering organic waste gas produced through dry process overlaying and after finishing of synthetic leather |
| CN210729094U (en) * | 2019-07-18 | 2020-06-12 | 成都云白环境设备制造有限公司 | Organic waste gas absorbs and recovery unit |
| CN217410282U (en) * | 2022-03-24 | 2022-09-13 | 广州金鹏环保工程有限公司 | Waste gas purification device and system for recycling absorption liquid |
-
2023
- 2023-04-10 CN CN202310369417.4A patent/CN116078118A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102179137A (en) * | 2011-05-05 | 2011-09-14 | 艾特克控股集团有限公司 | Method for treating organic waste gas |
| CN104801156A (en) * | 2015-04-09 | 2015-07-29 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Method for recovering organic waste gas produced through dry process overlaying and after finishing of synthetic leather |
| CN210729094U (en) * | 2019-07-18 | 2020-06-12 | 成都云白环境设备制造有限公司 | Organic waste gas absorbs and recovery unit |
| CN217410282U (en) * | 2022-03-24 | 2022-09-13 | 广州金鹏环保工程有限公司 | Waste gas purification device and system for recycling absorption liquid |
Non-Patent Citations (1)
| Title |
|---|
| 陈家庆编著: "《石油石化工业环保技术概论》", 中国石化出版社, pages: 352 - 353 * |
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Application publication date: 20230509 |